EP2406181B1 - Verfahren zur herstellung von phosgen - Google Patents
Verfahren zur herstellung von phosgen Download PDFInfo
- Publication number
- EP2406181B1 EP2406181B1 EP10707905.5A EP10707905A EP2406181B1 EP 2406181 B1 EP2406181 B1 EP 2406181B1 EP 10707905 A EP10707905 A EP 10707905A EP 2406181 B1 EP2406181 B1 EP 2406181B1
- Authority
- EP
- European Patent Office
- Prior art keywords
- carbon monoxide
- reactor
- stream
- feed stream
- phosgene
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
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Links
- YGYAWVDWMABLBF-UHFFFAOYSA-N Phosgene Chemical compound ClC(Cl)=O YGYAWVDWMABLBF-UHFFFAOYSA-N 0.000 title claims description 62
- 238000004519 manufacturing process Methods 0.000 title claims description 12
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 86
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 85
- 229910052801 chlorine Inorganic materials 0.000 claims description 40
- 239000000460 chlorine Substances 0.000 claims description 40
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 claims description 38
- 238000000034 method Methods 0.000 claims description 25
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 20
- 239000003054 catalyst Substances 0.000 claims description 20
- 238000006243 chemical reaction Methods 0.000 claims description 17
- 239000000203 mixture Substances 0.000 claims description 16
- 238000005259 measurement Methods 0.000 claims description 13
- 238000011144 upstream manufacturing Methods 0.000 claims description 9
- 239000007788 liquid Substances 0.000 claims description 8
- 238000009833 condensation Methods 0.000 claims description 7
- 230000005494 condensation Effects 0.000 claims description 7
- 238000005201 scrubbing Methods 0.000 claims description 5
- 238000000926 separation method Methods 0.000 claims description 3
- 238000001228 spectrum Methods 0.000 claims description 3
- 238000002156 mixing Methods 0.000 claims description 2
- 238000004886 process control Methods 0.000 claims description 2
- 230000001105 regulatory effect Effects 0.000 claims description 2
- 238000001816 cooling Methods 0.000 claims 1
- 239000007789 gas Substances 0.000 description 24
- 239000000047 product Substances 0.000 description 16
- 238000011049 filling Methods 0.000 description 8
- 239000011949 solid catalyst Substances 0.000 description 4
- 125000001309 chloro group Chemical group Cl* 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 238000010574 gas phase reaction Methods 0.000 description 3
- 238000004064 recycling Methods 0.000 description 3
- 239000002912 waste gas Substances 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 230000007797 corrosion Effects 0.000 description 2
- 239000012948 isocyanate Substances 0.000 description 2
- 150000002513 isocyanates Chemical class 0.000 description 2
- 239000010959 steel Substances 0.000 description 2
- 239000005057 Hexamethylene diisocyanate Substances 0.000 description 1
- 238000004566 IR spectroscopy Methods 0.000 description 1
- 239000003990 capacitor Substances 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- MVPPADPHJFYWMZ-UHFFFAOYSA-N chlorobenzene Chemical compound ClC1=CC=CC=C1 MVPPADPHJFYWMZ-UHFFFAOYSA-N 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- 125000005442 diisocyanate group Chemical group 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- RRAMGCGOFNQTLD-UHFFFAOYSA-N hexamethylene diisocyanate Chemical compound O=C=NCCCCCCN=C=O RRAMGCGOFNQTLD-UHFFFAOYSA-N 0.000 description 1
- 239000013067 intermediate product Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000004814 polyurethane Substances 0.000 description 1
- 229920002635 polyurethane Polymers 0.000 description 1
- 239000011541 reaction mixture Substances 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 239000007858 starting material Substances 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- DVKJHBMWWAPEIU-UHFFFAOYSA-N toluene 2,4-diisocyanate Chemical compound CC1=CC=C(N=C=O)C=C1N=C=O DVKJHBMWWAPEIU-UHFFFAOYSA-N 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B32/00—Carbon; Compounds thereof
- C01B32/80—Phosgene
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/26—Nozzle-type reactors, i.e. the distribution of the initial reactants within the reactor is effected by their introduction or injection through nozzles
Definitions
- the invention relates to a process for the production of phosgene by the gas phase reaction of carbon monoxide and chlorine in the presence of a solid catalyst and a process for the production of phosgene using the reactor.
- Phosgene is an important auxiliary material in the production of intermediate and end products in almost all branches of chemistry.
- the largest area of application in terms of quantity is the production of diisocyanates for polyurethane chemistry, in particular of tolylene diisocyanate, 4,4-diisocyanate-diphenylmethane and hexamethylene diisocyanate.
- Phosgene is produced on an industrial scale in a catalytic gas phase reaction of carbon monoxide and chlorine in the presence of a solid catalyst, preferably activated carbon.
- the reaction is strongly exothermic, the enthalpy of formation is -107.6 kJ / mol.
- the reaction is usually carried out in a tube bundle reactor according to the in Ullmann's Encyclopedia of Industrial Chemistry, Vol. A 19, pages 413 to 414 described method.
- the granular catalyst, with a particle size in the range from 3 to 5 mm, is then used in tubes with an internal diameter between 50 and 70 mm.
- the reaction starts at 40 to 50 ° C, the temperature in the pipes rises to around 400 ° C and then drops quickly.
- Carbon monoxide is used in a small excess to ensure that all of the chlorine is converted and to obtain chlorine-free phosgene.
- the reaction is usually carried out under pressure, frequently at 2 to 6 bar excess pressure.
- the US4231959 discloses a process for the production of phosgene from carbon monoxide and chlorine in a tube bundle reactor, with activated carbon as a catalyst and water as a coolant.
- the carbon monoxide is supplied in a stoichiometric excess compared to chlorine.
- the phosgene produced is partially separated by condensation and at least part of the waste gas stream (for the most part carbon monoxide) is recycled and reused as a starting material. Part of the exhaust gas flow is eliminated and cleaned.
- the DE 102 08 398 describes a tube bundle reactor and a method for the production of phosgene, according to which the corrosion problems in the deflection area of the heat carrier are reduced and thus an increased specific cross-sectional load and thus a higher capacity is made possible.
- a reactor for the production of phosgene by the gas phase reaction of carbon monoxide and chlorine in the presence of a solid catalyst with a bundle of contact tubes arranged parallel to one another, in the longitudinal direction of the reactor, which are attached at their ends in tube sheets, each with a hood at both ends of the Reactor, as well as with baffles arranged perpendicular to the longitudinal direction of the reactor in the space between the contact tubes, which alternately leave opposing passage openings on the inner wall of the reactor, the contact tubes being filled with the solid catalyst, the gaseous reaction mixture from one end of the reactor via a hood through the contact tubes passed and withdrawn from the opposite end of the reactor over the second hood and a liquid heat exchange medium is passed through the space around the contact tubes, to be designed in such a way that the reactor in the area of the passage openings is not drilled, the area between the free end of a baffle plate and the inner wall of the reactor under the passage opening is understood.
- Phosgene reactors are run to complete chlorine conversion, since the specification requirements for the subsequent use, in particular for the production of isocyanates, stipulate practically chlorine-free phosgene with residual chlorine contents of a maximum of 1000 ppm, or a maximum of 100 ppm, or a maximum of 10 ppm, especially since chlorine residues Negatively affect the color number of the isocyanates.
- the solution consists in a process for the production of phosgene by converting a feed stream obtained by combining and mixing a chlorine feed stream and a carbon monoxide feed stream, the carbon monoxide is fed in stoichiometric excess compared to chlorine, on catalyst tubes of a reactor with a bundle of catalyst tubes filled with activated carbon beds, while obtaining a product gas mixture, which is separated into a liquid, phosgene-containing product stream and an exhaust gas stream containing carbon monoxide, which is discharged via a pressure holding valve, and the conversion of the feed stream in the reactor and the separation of the product gas mixture under a pressure in the range from 2.0 to 6, 0 bar overpressure, which is characterized in that the carbon monoxide excess in the feed stream to the reactor is regulated by continuously measuring the flow rate and the concentration of carbon monoxide in the exhaust gas flow, from this in connection with the continuously recorded measured values for the flow rate of the carbon monoxide feed stream, the flow rate and the chlorine concentration of the chlorine feed stream, the The actual value for
- the mass flow and the chlorine concentration of the chlorine feed stream as well as the mass flow of the carbon monoxide feed stream are recorded continuously.
- the target value for the carbon monoxide excess in the feed stream to the reactor is state-dependent, i.e., taking into account the geometry of the activated charcoal beds, the phosgene load and the operating pressure, it is calculated on the basis of a reaction kinetic model that is validated by experimental measurements.
- variable to be controlled the carbon monoxide excess in the feed stream to the reactor, is continuously calculated, compared with the setpoint calculated or experimentally determined for the corresponding operating state and, in the sense of an adjustment to the setpoint, influenced via the manipulated variable, the mass flow of the carbon monoxide feed stream .
- the setpoint values calculated on the basis of a reaction kinetic model for the carbon monoxide excess in the feed stream are checked for plausibility by experimenting in a pilot reactor with a single contact tube, which has the same dimensions as the contact tubes of the reactor, under the same operating conditions as in the reactor, The contact tube is filled with activated carbon catalyst to different filling levels and a phosgene load spectrum is run through for each filling level, and a connected chlorine measurement determines at which excess carbon monoxide the chlorine breakthrough takes place.
- the actual values and the setpoint values for the carbon monoxide excess in the feed stream to the reactor are advantageously displayed in the process control system for the process. This means that the actual values can be adjusted to the target values either automatically or manually.
- the specific carbon monoxide consumption is further reduced by separating the phosgene product from the product gas mixture from the reactor and separating a substream from the remaining gas stream, which is returned as a recycle stream to the phosgene reactor.
- the recycling stream often still has a carbon monoxide concentration in the range from 20 to 60% by weight, preferably 30 to 50% by weight, based on the total weight of the recycling stream.
- the substream that is returned as a recycle stream upstream of the phosgene reactor can preferably amount to 40 to 95% by weight, preferably 75 to 90% by weight of the gas stream that remains from the product gas mixture after the liquid phosgene has been separated off.
- the recycling of the recycle stream upstream of the phosgene reactor is advantageously carried out via a propulsion jet nozzle which is driven by the inlet pressure of one of the two feed streams, the carbon monoxide feed stream or the chlorine feed stream.
- Liquid phosgene is separated off from the product gas mixture downstream of the phosgene reactor, preferably in two stages, by condensation.
- the remaining gas stream is preferably separated into a partial stream which is returned as a recycle stream upstream of the phosgene reactor and a residual stream from which phosgene is washed out in a scrubbing column, and a waste gas stream remains which is discharged from the plant.
- the phosgene stream from the scrubbing column can be combined with the product stream from the preferably two-stage condensation.
- the flow rate of the recycle flow is measured continuously and the carbon monoxide concentration of the recycle flow is continuously calculated from the measurement data for the flow rate and the carbon monoxide concentration of the exhaust gas flow in connection with the operating conditions of temperature and pressure of the condensation.
- These data i.e. the flow rate and the carbon monoxide concentration of the recycle stream, are continuously included in the calculation of the actual value for the carbon monoxide excess in the feed stream to the reactor.
- the flow rate of the exhaust gas flow upstream of the pressure control valve for discharging the exhaust gas flow from the system and the carbon monoxide concentration of the same after the pressure control valve, for example, measured by IR spectrometry.
- the measurement of the carbon monoxide concentration in the exhaust gas flow is much simpler and more precise than a measurement of the carbon monoxide concentration in the feed flow to the phosgene reactor;
- the flow rate is significantly lower and no measurement under increased pressure is required, in particular no pressure-resistant measuring cuvettes.
- the flow rate of the exhaust gas stream and the concentration of carbon monoxide in the exhaust gas stream are measured continuously after the pressure control valve.
- the reactor for converting carbon monoxide and chlorine to phosgene can preferably comprise a main reactor and a postreactor.
- a main reactor preferably a reactor and a postreactor.
- up to 10% residual conversion can be carried out in the postreactor, and the postreactor can be operated adiabatically or cooled.
- two parallel measuring devices can advantageously be provided downstream of the pressure holding valve, which are operated at different times so that there are no downtimes.
- the chlorine content of the product gas mixture downstream of the phosgene reactor can preferably also be measured at time intervals or continuously.
- the carbon monoxide excess in the feed stream can also be roughly adjusted on the basis of this measurement of the chlorine content of the product gas mixture downstream of the phosgene reactor; however, this type of chlorine measurement and reactor control is not very reliable.
- FIG. 1 shows a phosgene reactor R to which a chlorine feed stream, reference number 2, and a carbon monoxide feed stream, reference number 3, are fed as feed stream 1 after being combined and mixed in a static mixer M.
- the product gas mixture 4 from the reactor R is fed to two capacitors K connected in series. Liquid phosgene is separated from this as product stream 5, leaving a gas stream 7 which is divided into a recycle stream 8 and a residual stream 9.
- the recycle stream 8 is recycled upstream of the reactor R via a propulsion jet nozzle T which, in the embodiment shown in the figure, is driven, for example, via the pre-pressure of the carbon monoxide feed stream 3.
- the residual stream 9 is fed to a scrubbing column W, in which further valuable product phosgene is washed out with a suitable solvent, for example monochlorobenzene, leaving a waste gas stream 6 which is discharged from the plant.
- Figure 2 shows an operator diagram with a set of parameters showing the target values for the carbon monoxide excess in the feed stream as a function of the operating conditions Represents catalyst filling height in the catalyst tubes, phosgene load, pressure and temperature.
- the carbon monoxide excess, CO, in the feed stream to the phosgene reactor is indicated on the abscissa in percent, and the filling height of the catalyst tubes, h, in meters, on the ordinate.
- Curves I to VII denote different load conditions, each given in kg phosgene / m 2 / s: curve I corresponds to a phosgene load of 1.4, curve II to a phosgene load of 1.6, curve III to a phosgene load of 1.8, curve IV a phosgene load of 2.0, curve V a phosgene load of 2.2, curve VI a phosgene load of 2.4 and curve VII a phosgene load of 2.6.
- the operator diagram shown was created experimentally through tests in the following way:
- the starting point is a contact tube made of duplex steel 1.4462, customary in phosgene synthesis, with an outside diameter of 44.5 mm, a wall thickness of 2.6 mm and a length of 5 m.
- This is filled with activated carbon catalyst to different filling heights, starting with a filling height of 1.5 m in 0.25 m steps up to a maximum filling height of 4.5 m.
- the phosgene load spectrum of 1.4 to 2.6 kg phosgene / m 2 / s is run through in 0.2 kg phosgene / m 2 / s steps and a connected chlorine measurement determines the carbon monoxide excess at which the chlorine breakthrough takes place.
- the target value for the excess carbon monoxide for the respective operating state of the reactor can be approached much more closely to the limit.
- downtimes of the system can be avoided, which with considerable effort for the catalyst change - the catalyst change, i.e. emptying the catalyst tubes, cleaning, checking, refilling, making the catalyst phosgene-free and drying usually requires 12 to 17 working days.
- the running times of the contact tubes can be adjusted so that they fall within the maintenance intervals prescribed by law, generally 2 to 5 years.
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP10707905.5A EP2406181B1 (de) | 2009-03-11 | 2010-03-10 | Verfahren zur herstellung von phosgen |
Applications Claiming Priority (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP09154882 | 2009-03-11 | ||
EP09157407 | 2009-04-06 | ||
PCT/EP2010/053011 WO2010103029A1 (de) | 2009-03-11 | 2010-03-10 | Verfahren zur herstellung von phosgen |
EP10707905.5A EP2406181B1 (de) | 2009-03-11 | 2010-03-10 | Verfahren zur herstellung von phosgen |
Publications (2)
Publication Number | Publication Date |
---|---|
EP2406181A1 EP2406181A1 (de) | 2012-01-18 |
EP2406181B1 true EP2406181B1 (de) | 2020-10-28 |
Family
ID=42140219
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP10707905.5A Active EP2406181B1 (de) | 2009-03-11 | 2010-03-10 | Verfahren zur herstellung von phosgen |
Country Status (9)
Country | Link |
---|---|
US (1) | US8993803B2 (hu) |
EP (1) | EP2406181B1 (hu) |
JP (1) | JP5681121B2 (hu) |
KR (1) | KR101778312B1 (hu) |
CN (2) | CN105540589B (hu) |
ES (1) | ES2847290T3 (hu) |
HU (1) | HUE052073T2 (hu) |
PT (1) | PT2406181T (hu) |
WO (1) | WO2010103029A1 (hu) |
Families Citing this family (16)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
PT2421818E (pt) | 2009-04-24 | 2014-09-10 | Basf Se | Processo para a preparação de mda e mdi de cor estável |
US8841480B2 (en) | 2009-07-16 | 2014-09-23 | Basf Se | Process for the preparation of light-colored iocyanates of a diphenylmethanediisocyanate series |
CN102092713B (zh) * | 2010-12-13 | 2013-05-22 | 甘肃银光聚银化工有限公司 | 连续制备光气的方法 |
HUE025025T2 (hu) * | 2011-03-31 | 2016-04-28 | Basf Se | Eljárás izocianátok elõállítására |
CN104428247B (zh) | 2012-07-11 | 2017-03-29 | 科思创德国股份有限公司 | 用于产生碳酰氯的设备和方法 |
EP3024782B1 (en) * | 2013-07-26 | 2019-06-12 | SABIC Global Technologies B.V. | Method and apparatus for producing high purity phosgene |
CN105408250B (zh) | 2013-07-26 | 2018-08-07 | 沙特基础全球技术有限公司 | 用于生产高纯光气的方法和装置 |
EP2896597A1 (de) | 2014-01-21 | 2015-07-22 | Bayer MaterialScience AG | Verfahren zum An- und Abfahren eines Phosgengenerators |
CN105980346B (zh) | 2014-02-04 | 2018-05-18 | 沙特基础工业全球技术有限公司 | 生产碳酸酯的方法 |
US9670131B2 (en) | 2014-02-04 | 2017-06-06 | Sabic Global Technologies B.V. | Method for producing carbonates |
BR112018070938A2 (pt) * | 2016-05-10 | 2019-01-29 | Huntsman Int Llc | processos para fabricação de isocianatos e para preparação de compostos de policarbonato. |
EP3421426A1 (de) * | 2017-06-29 | 2019-01-02 | Covestro Deutschland AG | Energieeffizientes verfahren zur bereitstellung von phosgen-dampf |
CN113784917A (zh) | 2019-04-25 | 2021-12-10 | 巴斯夫欧洲公司 | 光气的制备方法 |
US20220332587A1 (en) * | 2019-05-20 | 2022-10-20 | Basf Se | Process and reactor for producing phosgene |
CN113402383A (zh) * | 2020-03-17 | 2021-09-17 | 上海祖玥新材料科技有限公司 | 一种2-乙基己酸与光气反应合成2-乙基己酰氯的方法 |
EP4326675A1 (en) | 2021-04-21 | 2024-02-28 | Basf Se | Process for preparing phosgene |
Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP0983792A1 (en) * | 1998-09-03 | 2000-03-08 | BP Chemicals Limited | Carbonylation process |
JP2003154235A (ja) * | 2001-11-21 | 2003-05-27 | Canon Inc | ガス処理装置及びガス処理方法 |
US20040181090A1 (en) * | 2003-03-14 | 2004-09-16 | Kenji Sanada | Method for managing operation of gas phase reaction apparatus |
EP1932828A2 (en) * | 2006-12-14 | 2008-06-18 | Bayer MaterialScience AG | Process for controlling a production process |
Family Cites Families (17)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR2109186A5 (en) * | 1970-10-06 | 1972-05-26 | France Etat | Phosgene - prepd from chlorine and excess carbon monoxide, - partially condensing product and recycling part of gaseous residue |
SE416760B (sv) * | 1977-08-23 | 1981-02-02 | Volvo Ab | Sett for bestemning eller styrning av en katalysators egenskaper och/eller forloppet av den av katalysatorn beroende reaktionen |
US4231959A (en) * | 1978-02-15 | 1980-11-04 | Stauffer Chemical Company | Phosgene manufacture |
US6022993A (en) * | 1996-02-21 | 2000-02-08 | E. I. Du Pont De Nemours And Company | Phosgene manufacturing process |
ES2163181T3 (es) * | 1996-06-28 | 2002-01-16 | Du Pont | Proceso de fabricacion de fosgeno. |
JP2000203824A (ja) * | 1999-01-08 | 2000-07-25 | Teijin Chem Ltd | ホスゲンの製造方法 |
JP4290793B2 (ja) * | 1999-01-22 | 2009-07-08 | 帝人化成株式会社 | ホスゲンの製造方法 |
DE19916856A1 (de) * | 1999-04-14 | 1999-09-23 | Eckert Gmbh Dr | Verfahren zur Herstellung von Carbonyldichlorid aus Chlor und Kohlenmonoxid |
US6399823B1 (en) * | 2001-04-30 | 2002-06-04 | General Electric Company | Method for producing phosgene |
DE50301676D1 (de) | 2002-02-27 | 2005-12-22 | Basf Ag | Verfahren zur herstellung von phosgen |
US7250530B2 (en) * | 2003-07-30 | 2007-07-31 | General Electric Company | Processes and systems for making phosgene |
JP4519609B2 (ja) * | 2004-03-23 | 2010-08-04 | エステー株式会社 | 脱臭除湿剤及び脱臭除湿器 |
JP4553674B2 (ja) * | 2004-10-15 | 2010-09-29 | 住友化学株式会社 | 塩素ガスの除害方法 |
DE102007057462A1 (de) | 2007-11-29 | 2009-06-10 | Bayer Materialscience Ag | Verfahren zur Herstellung von Phosgen mit reduzierter CO-Emission |
JP5336828B2 (ja) * | 2008-12-02 | 2013-11-06 | 三井化学株式会社 | 塩化カルボニルの製造方法および製造装置、ならびに、ポリイソシアネートの製造方法および製造装置 |
ES2656791T3 (es) | 2008-12-16 | 2018-02-28 | Basf Se | Reactor y procedimiento para la producción de fosgeno |
US8492587B2 (en) | 2008-12-16 | 2013-07-23 | Basf Se | Reactor and process for preparing phosgene |
-
2010
- 2010-03-10 ES ES10707905T patent/ES2847290T3/es active Active
- 2010-03-10 HU HUE10707905A patent/HUE052073T2/hu unknown
- 2010-03-10 US US13/255,665 patent/US8993803B2/en active Active
- 2010-03-10 JP JP2011553437A patent/JP5681121B2/ja not_active Expired - Fee Related
- 2010-03-10 CN CN201510849515.3A patent/CN105540589B/zh active Active
- 2010-03-10 PT PT107079055T patent/PT2406181T/pt unknown
- 2010-03-10 KR KR1020117023828A patent/KR101778312B1/ko active IP Right Grant
- 2010-03-10 EP EP10707905.5A patent/EP2406181B1/de active Active
- 2010-03-10 WO PCT/EP2010/053011 patent/WO2010103029A1/de active Application Filing
- 2010-03-10 CN CN2010800118855A patent/CN102348639A/zh active Pending
Patent Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP0983792A1 (en) * | 1998-09-03 | 2000-03-08 | BP Chemicals Limited | Carbonylation process |
JP2003154235A (ja) * | 2001-11-21 | 2003-05-27 | Canon Inc | ガス処理装置及びガス処理方法 |
US20040181090A1 (en) * | 2003-03-14 | 2004-09-16 | Kenji Sanada | Method for managing operation of gas phase reaction apparatus |
EP1932828A2 (en) * | 2006-12-14 | 2008-06-18 | Bayer MaterialScience AG | Process for controlling a production process |
Also Published As
Publication number | Publication date |
---|---|
KR101778312B1 (ko) | 2017-09-13 |
CN105540589A (zh) | 2016-05-04 |
WO2010103029A1 (de) | 2010-09-16 |
EP2406181A1 (de) | 2012-01-18 |
ES2847290T3 (es) | 2021-08-02 |
KR20110138366A (ko) | 2011-12-27 |
PT2406181T (pt) | 2020-12-24 |
HUE052073T2 (hu) | 2021-04-28 |
US20110319662A1 (en) | 2011-12-29 |
CN102348639A (zh) | 2012-02-08 |
US8993803B2 (en) | 2015-03-31 |
JP2012520228A (ja) | 2012-09-06 |
JP5681121B2 (ja) | 2015-03-04 |
CN105540589B (zh) | 2018-12-04 |
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